CA1239366A - Guiding hydrogenation gas into coal liquefaction plants - Google Patents
Guiding hydrogenation gas into coal liquefaction plantsInfo
- Publication number
- CA1239366A CA1239366A CA000472170A CA472170A CA1239366A CA 1239366 A CA1239366 A CA 1239366A CA 000472170 A CA000472170 A CA 000472170A CA 472170 A CA472170 A CA 472170A CA 1239366 A CA1239366 A CA 1239366A
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- Canada
- Prior art keywords
- oil
- refining
- hydrogenation
- coal
- hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
According to the present invention, a most advantageous hydro-genating gas system for a coal liquification plant is achieved in that the hydrogen-rich gases that occur in the subsequent refinement stages are not divided into circulating and excess gas, but are supplied to the freshly generated hydrogen of the hydrogenation stage as a total quantity.
According to the present invention, a most advantageous hydro-genating gas system for a coal liquification plant is achieved in that the hydrogen-rich gases that occur in the subsequent refinement stages are not divided into circulating and excess gas, but are supplied to the freshly generated hydrogen of the hydrogenation stage as a total quantity.
Description
~39;~ 26982-20 A Hydrogenation Gas Routing in Coal Liquefaction Plants The present invention relates to a hydrogenation gas routing in coal liquefaction plants, whereby the light and medium oil that is obtained is being refined after hydrogenation.
orally, dried coal is mashed with solvent and hydra-jointed by the addition of hydrogen. The products are separated in the separators that follow the hydrogenation reactors. In hot separators, the gases and vapors are drawn off at the head, form a sup a liquid phase that contains the solids is drawn off to a vacuum distillation.
The head product of the hot separator is passed to a subsequent cold separator after cooling. In addition to the coal oil water occurs here as the liquid phase from which valuable contents (ammonia, phenol) are extracted in the subsequent stages of the process.
The gas phase of the cold separator, which exits at the head, is divide dafter oil washing that is conducted at process pressure into circulating and output gas. The circulating gas is returned to the hydrogenation after compensation for pressure loss with a circulation-gas compressor. The output is cleaned in a gas washer and broken down in a low temperature decomposition unit into hydrogen, heating gas, SAG, and LUG. The hydrogen fraction is mixed with the newly generated hydrogen of the hydrogenation.
' ' ' ' ' The coal oil is broken down into light, medium and heavy oil in atmospheric distillation. The heavy oil is returned to the mashing stage as solvent.
The light and medium oil fractions are in each instance subjected to hydrogenating refinement for purposes of removing sulfur, nitrogen, and similar undesirable components. To this end, after the addition of hydrogen the crude light or crude medium oil is vaporized and passed to solid-bed reactors. The refinement is carried out on the Comma or Nemo catalyst layers.
In order to limit the temperature increase that is governed by the reaction heat of the hydrogenation, quenching hydrogen is channeled into the hydrogenation reactors. The emerging, refined products are cooled in heat exchangers and by the injection of quench water, and separated into refined product, water and gas in separators. The state of the art is to return a part of the H2-rich excess gas to the newly generated hydrogen of the refinement as circulating gas after compensation for the pressure loss with a circulating gas compressor, and to tap off the other excess amounts of gas for cleaning and extraction of the hydrogen and the gaseous hydrocarbons and return them to the appropriate stages of the process.
The residue from the hot separator, which contains the solids, is topped in a vacuum distillation. The heavy oil that is extracted is returned, together with heavy and medium oil from the atmosphere distillation, as a solvent, where it is used in the mashing process.
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orally, dried coal is mashed with solvent and hydra-jointed by the addition of hydrogen. The products are separated in the separators that follow the hydrogenation reactors. In hot separators, the gases and vapors are drawn off at the head, form a sup a liquid phase that contains the solids is drawn off to a vacuum distillation.
The head product of the hot separator is passed to a subsequent cold separator after cooling. In addition to the coal oil water occurs here as the liquid phase from which valuable contents (ammonia, phenol) are extracted in the subsequent stages of the process.
The gas phase of the cold separator, which exits at the head, is divide dafter oil washing that is conducted at process pressure into circulating and output gas. The circulating gas is returned to the hydrogenation after compensation for pressure loss with a circulation-gas compressor. The output is cleaned in a gas washer and broken down in a low temperature decomposition unit into hydrogen, heating gas, SAG, and LUG. The hydrogen fraction is mixed with the newly generated hydrogen of the hydrogenation.
' ' ' ' ' The coal oil is broken down into light, medium and heavy oil in atmospheric distillation. The heavy oil is returned to the mashing stage as solvent.
The light and medium oil fractions are in each instance subjected to hydrogenating refinement for purposes of removing sulfur, nitrogen, and similar undesirable components. To this end, after the addition of hydrogen the crude light or crude medium oil is vaporized and passed to solid-bed reactors. The refinement is carried out on the Comma or Nemo catalyst layers.
In order to limit the temperature increase that is governed by the reaction heat of the hydrogenation, quenching hydrogen is channeled into the hydrogenation reactors. The emerging, refined products are cooled in heat exchangers and by the injection of quench water, and separated into refined product, water and gas in separators. The state of the art is to return a part of the H2-rich excess gas to the newly generated hydrogen of the refinement as circulating gas after compensation for the pressure loss with a circulating gas compressor, and to tap off the other excess amounts of gas for cleaning and extraction of the hydrogen and the gaseous hydrocarbons and return them to the appropriate stages of the process.
The residue from the hot separator, which contains the solids, is topped in a vacuum distillation. The heavy oil that is extracted is returned, together with heavy and medium oil from the atmosphere distillation, as a solvent, where it is used in the mashing process.
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Synthesis gas (C0 + Ho) or, after hydrogenation and gas washing, hydrogenating hydrogen is obtained in a gasification stage.
If the hydrogen that is either returned or obtained through residual gasification, low temperature fractionation or circulation gas is insufficient for hydrogenation and stubbles-lion, the shortfall can be made up by coal gasification with subsequent conversion and gas cleaning, or by external procure-mint.
It is the task of the present invention to simplify hydrogenating gas supply and improve it from the point of view of economy.
According to the present invention, the total quantity of the gases resulting in the refining stages is supplied to the newly generated hydrogen of the hydrogenation stage. That is to say, there is no division of the hydrogen-rich gases coming from the refining stages into circulating and excess gas, the total quantity being passed to hydrogenation. The organic (Of- C4) and inorganic (C0, C02, HIS) gaseous compounds that occur during refining and are contained in the gas in addition to hydrogen have no effect on the hydrogenation of the coal in the concentrations that exist here.
According to the present invention there is further provided a method of coal liquefaction comprising the steps of:
a) mashing incoming coal with solvent;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
Synthesis gas (C0 + Ho) or, after hydrogenation and gas washing, hydrogenating hydrogen is obtained in a gasification stage.
If the hydrogen that is either returned or obtained through residual gasification, low temperature fractionation or circulation gas is insufficient for hydrogenation and stubbles-lion, the shortfall can be made up by coal gasification with subsequent conversion and gas cleaning, or by external procure-mint.
It is the task of the present invention to simplify hydrogenating gas supply and improve it from the point of view of economy.
According to the present invention, the total quantity of the gases resulting in the refining stages is supplied to the newly generated hydrogen of the hydrogenation stage. That is to say, there is no division of the hydrogen-rich gases coming from the refining stages into circulating and excess gas, the total quantity being passed to hydrogenation. The organic (Of- C4) and inorganic (C0, C02, HIS) gaseous compounds that occur during refining and are contained in the gas in addition to hydrogen have no effect on the hydrogenation of the coal in the concentrations that exist here.
According to the present invention there is further provided a method of coal liquefaction comprising the steps of:
a) mashing incoming coal with solvent;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
- 3 -I' c) refining said products of hydrogenation in a plurality of stages to obtain hydrogen-rich gases and other products comprising coal oil; and d) recycling substantially all of said hydrogen-rich gases, from at least a predetermined one of said plurality of stages, produced in step c) back to the said hydrogenation step for hydrogenation of said incoming coal.
Preferably step c) includes distilling of oil into fractions and recycling substantially all of the hydrogen-rich gases obtained back from said distilling to said hydrogenation step. Also, preferably step c) includes hot separating the products of hydrogenation, and then cold separating output products from said hot separating step, and then at least collecting a portion of gases collected from an output of said cold separating step back to said hydrogenation step.
Particularly preferred in step c) is distilling of oil into fractions and recycling substantially all of the hydrogen-rich gases obtained from said distilling back to said hydrogenation step.
Preferably when distilling oil into fractions and light oil and medium oil are produced. These oils are then refined further in separate stages for the light and medium oils (particular preferred in each case is atmospheric distilling) and substantially all the hydrogen rich gases from each separate refining stage are recycled back to the hydrogenation step.
A preferred embodiment of the invention comprises a method of coal liquefaction comprising the steps of:
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Preferably step c) includes distilling of oil into fractions and recycling substantially all of the hydrogen-rich gases obtained back from said distilling to said hydrogenation step. Also, preferably step c) includes hot separating the products of hydrogenation, and then cold separating output products from said hot separating step, and then at least collecting a portion of gases collected from an output of said cold separating step back to said hydrogenation step.
Particularly preferred in step c) is distilling of oil into fractions and recycling substantially all of the hydrogen-rich gases obtained from said distilling back to said hydrogenation step.
Preferably when distilling oil into fractions and light oil and medium oil are produced. These oils are then refined further in separate stages for the light and medium oils (particular preferred in each case is atmospheric distilling) and substantially all the hydrogen rich gases from each separate refining stage are recycled back to the hydrogenation step.
A preferred embodiment of the invention comprises a method of coal liquefaction comprising the steps of:
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' ' lZ39366 26982-20 a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation:
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining including distilling said coal oil into at least a light oil fraction and a medium oil fraction which oil fractions are refined further in a separate stage for the light oil and a separate stage for the medium oil; and e) recycling back substantially all of said hydrogen-rich gases from said light oil refining stage and said : medium oil refining stage to said hydrogenation step.
Another preferred embodiment of the invention comprises a method of coal liquefaction comprising the steps of:
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining of said products of hydrogenation including further refining of said coal oil into at least a first oil fraction and a second oil fraction which oil fractions are refined further in a separate stage for the first oil fraction and a separate stage for the second oil fraction; and : I;
' ' lZ39366 26982-20 a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation:
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining including distilling said coal oil into at least a light oil fraction and a medium oil fraction which oil fractions are refined further in a separate stage for the light oil and a separate stage for the medium oil; and e) recycling back substantially all of said hydrogen-rich gases from said light oil refining stage and said : medium oil refining stage to said hydrogenation step.
Another preferred embodiment of the invention comprises a method of coal liquefaction comprising the steps of:
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining of said products of hydrogenation including further refining of said coal oil into at least a first oil fraction and a second oil fraction which oil fractions are refined further in a separate stage for the first oil fraction and a separate stage for the second oil fraction; and : I;
- 5 -. , .
:
~393~6 e) recycling back substantially all of said hydrogen-rich gases from said first oil refining stage and said second oil refining stage to said hydrogenation step.
According to the division of the gas phase from the cold separator into circulation and output gas, it is either extracted or channeled off through the gas wash and low-temperature fractionation stage with the same gaseous compounds that result additionally during hydrogenation of the coal.
The omission of dedicated circulating gas compressors, gas washers and hydrogen reclamation stages for refining the light and medium oil is a significant advantage vis-a-vis investment and operation.
The invention will be further described with reference to the accompanying drawing which is a flow diagram of a hydrogenating gas system according to the invention.
Dried coal is mashed with solvent in a mashing stage (1) and hydrogenated in a reactor (2) during the addition of hydrogen.
Phase separation takes place in a hot separator (3) that follows the hydrogenation reactor (2). The gases and the vapors are 20 drawn off at the head. The liquid phase that contains the solids is drawn off for vacuum distillation (5) from the sup.
After cooling, the head product from the hot separator is passed to a cold separator (4). Water as well as COAL OIL
occur here, and the water is pumped off separately for reextraction of the valuable contents such as ammonia and phenol.
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~393~6 e) recycling back substantially all of said hydrogen-rich gases from said first oil refining stage and said second oil refining stage to said hydrogenation step.
According to the division of the gas phase from the cold separator into circulation and output gas, it is either extracted or channeled off through the gas wash and low-temperature fractionation stage with the same gaseous compounds that result additionally during hydrogenation of the coal.
The omission of dedicated circulating gas compressors, gas washers and hydrogen reclamation stages for refining the light and medium oil is a significant advantage vis-a-vis investment and operation.
The invention will be further described with reference to the accompanying drawing which is a flow diagram of a hydrogenating gas system according to the invention.
Dried coal is mashed with solvent in a mashing stage (1) and hydrogenated in a reactor (2) during the addition of hydrogen.
Phase separation takes place in a hot separator (3) that follows the hydrogenation reactor (2). The gases and the vapors are 20 drawn off at the head. The liquid phase that contains the solids is drawn off for vacuum distillation (5) from the sup.
After cooling, the head product from the hot separator is passed to a cold separator (4). Water as well as COAL OIL
occur here, and the water is pumped off separately for reextraction of the valuable contents such as ammonia and phenol.
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39~
The COAL OIL is drawn off and atmospherically distilled during the addition of strip steam in an atmospheric distillation stage (6). Light and medium oil from the atmospheric distillation stage are in each instance passed separately to refining stages (21, 22).
The gas phase that exits from the top of the cold separator is divided in a oil washing stage (7) into returned circulating gas and output gas is cleaned in a gas wash I and broken down in a low temperature fractionating plant into hydrogen, heating gas, SUNG and LUG.
The liquid phase formed in the hot separator contains the solids and is topped in the vacuum distillation stage (5).
The heavy oil so extracted is returned to the mashing stage (1) together with heavy and medium oil from the atmospheric distillation as solvent.
Synthesis gas (CO + Ho) is obtained in a gasification stage (10) or Hydrogenating hydrogen is obtained in a conversion and gas wash stage (11) from the residue of the vacuum distillation.
If the hydrogen that is returned through circulating gas, low temperature fractionation (9) and residue gasification (10) it insufficient for hydrogenation, the shortfall is made up through additional coal gasification (12) with subsequent conversion and gas wash stage (13).
The waste water from the cold separator, which contains tar acid of the atmospheric distillation stage is passed to an ammonia extraction stage (23) and a phenol extraction stage (24).
I; - 7 -.'' - ' ' .
, ~3~33~6 After biological processing (25) the waste water is run off into the public sewer system. The waste water that occurs during gasification (12) is run off in the same manner, and the waste water that occurs from gasification of the residue (10) is run off into the public sewer system after it has been neutralized (26).
The circulation gas that occurs from the oil wash (7) is compressed to the required operating pressure by means of a circulating-gas compressor (27). In addition to the circulating gas and the freshly generated hydrogen from the low-temperature fractionation the total quantity for the hydrogen-rich gases that emerge from the refining stages (21, 22) are supplied once again.
A mixture of these gases is supplied to the hydrogenation stage (2) and compressed to the pressure required for hydrogenation by means of a compressor (28).
Example In a coal liquification plant used for hydrogenation of a gas flame coal in the Wrier, with a throughput of 5,000 t (way) coal/day, some 31,833 kg/h crude light and 64,006 kg/h crude medium oil occur in the atmospheric distillation, this corresponding to an hourly output of approximately 208 t/h.
The refinement of the crude light oil takes place in two stages with the addition of 3,138 kg/h (stage I) and 2,587 kg/h (stage II) hydrogen at a purity of vowel at 60 bar. In the ; separators that follow the refining reactors the hydrogen-rich gas phase (total quantity 5,629 kg/h) is separated from the : `
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:
.
.
.
hydrogenation product at 55 bar. The total quantity of gas is passed directly to the hydrogenating gas.
Refinement of the crude medium oil takes place in one stage with the addition of 9,873 kg/h hydrogen (vowel), also at 60 bar. The gas that occurs in the subsequent separator (9,565 kg/h) is once again passed directly to the coal hydrogenation stage.
By enrichment at Of - C4 - hydrocarbon gas fractions as well as at C0 - C02 and HIS quantities the hydrogen content of the hydrogenating gas flowing through the refining stages falls to vowel in the case of light oil, or to vowel in the case of medium oil.
These Ho partial pressures lie essentially above that of the hydrogenating gas of the coal hydrogenation (216,252) kg/h, vowel), so that the feed presents no problems.
I, .
I
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The COAL OIL is drawn off and atmospherically distilled during the addition of strip steam in an atmospheric distillation stage (6). Light and medium oil from the atmospheric distillation stage are in each instance passed separately to refining stages (21, 22).
The gas phase that exits from the top of the cold separator is divided in a oil washing stage (7) into returned circulating gas and output gas is cleaned in a gas wash I and broken down in a low temperature fractionating plant into hydrogen, heating gas, SUNG and LUG.
The liquid phase formed in the hot separator contains the solids and is topped in the vacuum distillation stage (5).
The heavy oil so extracted is returned to the mashing stage (1) together with heavy and medium oil from the atmospheric distillation as solvent.
Synthesis gas (CO + Ho) is obtained in a gasification stage (10) or Hydrogenating hydrogen is obtained in a conversion and gas wash stage (11) from the residue of the vacuum distillation.
If the hydrogen that is returned through circulating gas, low temperature fractionation (9) and residue gasification (10) it insufficient for hydrogenation, the shortfall is made up through additional coal gasification (12) with subsequent conversion and gas wash stage (13).
The waste water from the cold separator, which contains tar acid of the atmospheric distillation stage is passed to an ammonia extraction stage (23) and a phenol extraction stage (24).
I; - 7 -.'' - ' ' .
, ~3~33~6 After biological processing (25) the waste water is run off into the public sewer system. The waste water that occurs during gasification (12) is run off in the same manner, and the waste water that occurs from gasification of the residue (10) is run off into the public sewer system after it has been neutralized (26).
The circulation gas that occurs from the oil wash (7) is compressed to the required operating pressure by means of a circulating-gas compressor (27). In addition to the circulating gas and the freshly generated hydrogen from the low-temperature fractionation the total quantity for the hydrogen-rich gases that emerge from the refining stages (21, 22) are supplied once again.
A mixture of these gases is supplied to the hydrogenation stage (2) and compressed to the pressure required for hydrogenation by means of a compressor (28).
Example In a coal liquification plant used for hydrogenation of a gas flame coal in the Wrier, with a throughput of 5,000 t (way) coal/day, some 31,833 kg/h crude light and 64,006 kg/h crude medium oil occur in the atmospheric distillation, this corresponding to an hourly output of approximately 208 t/h.
The refinement of the crude light oil takes place in two stages with the addition of 3,138 kg/h (stage I) and 2,587 kg/h (stage II) hydrogen at a purity of vowel at 60 bar. In the ; separators that follow the refining reactors the hydrogen-rich gas phase (total quantity 5,629 kg/h) is separated from the : `
I, .
:
.
.
.
hydrogenation product at 55 bar. The total quantity of gas is passed directly to the hydrogenating gas.
Refinement of the crude medium oil takes place in one stage with the addition of 9,873 kg/h hydrogen (vowel), also at 60 bar. The gas that occurs in the subsequent separator (9,565 kg/h) is once again passed directly to the coal hydrogenation stage.
By enrichment at Of - C4 - hydrocarbon gas fractions as well as at C0 - C02 and HIS quantities the hydrogen content of the hydrogenating gas flowing through the refining stages falls to vowel in the case of light oil, or to vowel in the case of medium oil.
These Ho partial pressures lie essentially above that of the hydrogenating gas of the coal hydrogenation (216,252) kg/h, vowel), so that the feed presents no problems.
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Claims (24)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. Hydrogenating gas system in a coal liquefication plant, hydrogenation following refinement of the oils that are extracted, characterized in that the total quantity of the gases that occur during refinement are supplied to the freshly generated hydrogen of the hydrogenation.
2. A coal liquification process in which coal is hydrogenated to produce oils which are in turn hydrogenated, the process comprising using all the gases out effluent from hydrogenation of the oil products as a source of hydrogen for the coal hydrogenation.
3. A process according to claim 1 or 2, wherein the oil products of the coal hydrogenation are divided at least into a light oil fraction and a medium oil fraction and said light and medium oil fractions are hydrogenated separately.
4. A process according to claim 1 or 2, wherein the oil products of the coal hydrogenation are divided into a heavy oil fraction, a medium oil fraction, and a light oil fraction, wherein the heavy oil fraction is used as a source of solvent for the coal in the coal hydrogenation, and wherein the medium and light oil fractions are each hydrogenated separately.
. 5. A method of coal liquefaction comprising the steps of:
a) mashing incoming coal with a solvent;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain hydrogen-rich gases and other products comprising coal oil; and d) recycling substantially all of said hydrogen-rich gases, from at least a predetermined one of said plurality of stages, produced in step c) back to the said hydrogenation step for hydrogenation of said incoming coal.
a) mashing incoming coal with a solvent;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain hydrogen-rich gases and other products comprising coal oil; and d) recycling substantially all of said hydrogen-rich gases, from at least a predetermined one of said plurality of stages, produced in step c) back to the said hydrogenation step for hydrogenation of said incoming coal.
6. A method according to claim 5, wherein said refining in step c) inclu-des distilling of oil into fractions and recycling substantially all of the hyd-rogen-rich gases obtained back from said distilling to said hydrogenation step.
7. A method according to claim 5, wherein said refining in step c) inclu-des hot separating the products of hydrogenation, and then cold separating output products from said hot separating step, and then at least collecting a portion of gases collected from an output of said cold separating step back to said hydro-genation step.
8. A method according to claim 7, wherein said refining in step c) inclu-des distilling of oil into fractions and recycling substantially all of the hyd-rogen-rich gases obtained from said distilling back to said hydrogenation step.
9. A method according to claim 6, wherein said distilling of oil into fractions produces light oil and medium oil which oils are refined further in a separate stage for the light oil and a separate stage for the medium oil and sub-stantially all of said hydrogen-rich gases from said light oil refining stage and said medium oil refining stage are recycled back to said hydrogenation step.
10. A method according to claim 7, wherein said distilling of oil into fractions produces light oil and medium oil which oils are refined further in a separate stage for the light oil and a separate stage for the medium oil and sub-stantially all of said hydrogen-rich gases from said light oil refining stage and said medium oil refining stage are recycled back to said hydrogenation step.
11. A method according to claim 8, wherein said distilling of oil into fractions produces light oil and medium oil which oils are refined further in a separate stage for the light oil and a separate stage for the medium oil and sub-staunchly all of said hydrogen-rich gases from said light oil refining stage and said medium oil refining stage are recycled back to said hydrogenation step.
12. A method according to claim 9, wherein said refining in said separate stage for said light oil is atmospheric distilling.
13. A method according to claim 10, wherein said refining in said separate stage for said light oil is atmospheric distilling.
14. A method according to claim 11, wherein said refining in said separate stage for said light oil is atmospheric distilling.
15. A method according to claim 9, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
16. A method according to claim 10, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
17. A method according to claim 11, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
18. A method according to claim 12, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
19. A method according to claim 13, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
20. A method according to claim 14, wherein said refining in said separate stage for said medium oil is atmospheric distilling.
21. A method of coal liquefaction comprising the steps of:
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining including distilling said coal oil into at least a light oil fraction and a medium oil fraction which oil fractions are refined further in a separate stage for the light oil and a separate stage for the medium oil; and e) recycling back substantially all of said hydrogen-rich gases from said light oil refining stage and said medium oil refining stage to said hydro-genation step.
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen-rich gases are produced;
d) said refining including distilling said coal oil into at least a light oil fraction and a medium oil fraction which oil fractions are refined further in a separate stage for the light oil and a separate stage for the medium oil; and e) recycling back substantially all of said hydrogen-rich gases from said light oil refining stage and said medium oil refining stage to said hydro-genation step.
22. A method according to claim 21, including recycling substantially all of the hydrogen-rich gases obtained from predetermined ones of said stages of said plurality of stages back to said hydrogenation step.
23. A method of coal liquefaction comprising the steps of:
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen rich gases are produced;
d) said refining of said products of hydrogenation including further refining of said coal oil into at least a first oil fraction and a second oil fraction which oil fractions are refined further in a separate stage for the first oil fraction and a separate stage for the second oil fraction; and e) recycling back substantially all of said hydrogen-rich gases from said first oil refining stage and said second oil refining stage to said hydro-genation step.
a) mashing incoming coal;
b) hydrogenating the mashed coal from step a) with hydrogen to produce products of hydrogenation;
c) refining said products of hydrogenation in a plurality of stages to obtain coal oil whereby hydrogen rich gases are produced;
d) said refining of said products of hydrogenation including further refining of said coal oil into at least a first oil fraction and a second oil fraction which oil fractions are refined further in a separate stage for the first oil fraction and a separate stage for the second oil fraction; and e) recycling back substantially all of said hydrogen-rich gases from said first oil refining stage and said second oil refining stage to said hydro-genation step.
24. A method according to claim 23, including recycling substantially all of the hydrogen-rich gases obtained from predetermined ones of said stages of said plurality of stages back to said hydrogenation step.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3401650.3 | 1984-01-19 | ||
| DE19843401650 DE3401650A1 (en) | 1983-12-10 | 1984-01-19 | Hydrogenation gas arrangement in coal liquefaction plants |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1239366A true CA1239366A (en) | 1988-07-19 |
Family
ID=6225291
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000472170A Expired CA1239366A (en) | 1984-01-19 | 1985-01-18 | Guiding hydrogenation gas into coal liquefaction plants |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0151399B1 (en) |
| JP (1) | JPS60161483A (en) |
| AU (1) | AU582133B2 (en) |
| BR (1) | BR8500578A (en) |
| CA (1) | CA1239366A (en) |
| DD (1) | DD236340A5 (en) |
| DE (1) | DE3572001D1 (en) |
| PL (1) | PL141658B1 (en) |
| SU (1) | SU1473714A3 (en) |
| ZA (1) | ZA85428B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3519830A1 (en) * | 1985-06-03 | 1986-12-18 | Ruhrkohle Ag, 4300 Essen | METAL OF COAL HYDRATION WITH INTEGRATED REFINING STAGES |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4179352A (en) * | 1975-08-07 | 1979-12-18 | Exxon Research & Engineering Co. | Coal liquefaction process |
| JPS5681390A (en) * | 1979-12-07 | 1981-07-03 | Chiyoda Chem Eng & Constr Co Ltd | Multistage hydrogenation treatment of coal |
| US4400263A (en) * | 1981-02-09 | 1983-08-23 | Hri, Inc. | H-Coal process and plant design |
| CA1199293A (en) * | 1982-06-17 | 1986-01-14 | Chevron Research And Technology Company | Two-stage hydroprocessing of heavy oils with recycle of residua |
-
1985
- 1985-01-12 EP EP85100277A patent/EP0151399B1/en not_active Expired
- 1985-01-12 DE DE8585100277T patent/DE3572001D1/en not_active Expired
- 1985-01-16 AU AU37720/85A patent/AU582133B2/en not_active Ceased
- 1985-01-16 JP JP60004178A patent/JPS60161483A/en active Pending
- 1985-01-17 PL PL1985251583A patent/PL141658B1/en unknown
- 1985-01-18 DD DD85272651A patent/DD236340A5/en unknown
- 1985-01-18 ZA ZA85428A patent/ZA85428B/en unknown
- 1985-01-18 SU SU853837677A patent/SU1473714A3/en active
- 1985-01-18 CA CA000472170A patent/CA1239366A/en not_active Expired
- 1985-02-08 BR BR8500578A patent/BR8500578A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| EP0151399A3 (en) | 1987-05-13 |
| AU3772085A (en) | 1985-07-25 |
| EP0151399B1 (en) | 1989-08-02 |
| PL251583A1 (en) | 1985-11-05 |
| PL141658B1 (en) | 1987-08-31 |
| EP0151399A2 (en) | 1985-08-14 |
| ZA85428B (en) | 1986-04-30 |
| DE3572001D1 (en) | 1989-09-07 |
| SU1473714A3 (en) | 1989-04-15 |
| JPS60161483A (en) | 1985-08-23 |
| AU582133B2 (en) | 1989-03-16 |
| DD236340A5 (en) | 1986-06-04 |
| BR8500578A (en) | 1985-09-24 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |